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Two_phase_beggs_brill.xlsx
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2 Phase Fluid

Two Phase Flow - Beggs & Brill Method
CheGuide.com Line Number P-10001
Chemical Engineer's Guide Description Feed Pipe
Date 30-Aug-15
User Input By CheGuide
Pipe Data Metric English
Inner Diameter 50.67 mm 1.995 inch
Pipe Roughness 0.00180 mm 0.000071 inch
Pipe Length 100.00 m 328.084 foot
Flow Direction uphill
Pipe Inclination angle 90 ° with horizontal
Gas
Flowing Temperature 32.2 Deg C 90.00 Deg F
Inlet Pressure 119 bar 1719.7 psi
Volumetric flowrate 9.0 m3/h 5.31 ft3/min
@ Standard Conditions 944.9 Nm3/h @ 1 atm, 0°C 587.6 SCFM @ 14.7 PSI, 60°F
Density 141.3 Kg/m3 8.823 lb/ft3
Viscosity 0.020 cP 1.34E-05 lb/ft.s
Liquid
Volumetric flowrate 4.75 m3/h 20.916 US gpm
Density 613.8 Kg/m3 38.320 lb/ft3
Viscosity 0.500 cP 3.36E-04 lb/ft.s
gas/liquid Surface tension 28.0 dyne/cm
Results
Flow pattern map Intermittent
Pressure drop due to head
Holdup volume fraction, EL(0) 0.462 0.462
Inclination correction factor, β 1.055 1.055
Inclined holdup v.f, EL(θ) 0.487 0.487
Mixture density 371.61 Kg/m3 23.20 lb/ft3
DP due to Head 3.64 bar 52.85 psi
Pressure drop due to friction
Friction factor ratio 1.445 1.445
No Slip Reynold's Number 157713 157713
No Slip friction factor, fNS 0.0042 Fanning 0.0042 Fanning
Two phase firction factor, fTP 0.0060 Fanning 0.0060 Fanning
DP due to friction 0.26 bar 3.77 psi
Total pressure drop 3.90 bar 56.62 psi
Correction due to acceleration 0.989 0.989
Corrected Total Pressure drop 3.95 bar 57.23 psi
Pressure drop / Length 3.95 bar / 100 mt 17.44 psi / 100 ft
Calculation (In English Units)
Area of Pipe 0.0217 ft2
Gravity constant, g 32.174 ft/s2
Liquid Gas
Flowrate 0.0466000002 ft3/s 0.08855 ft3/s
Superficial Velocity 2.147 ft/s 4.079 ft/s
Weight Flux, G 82.26 lb/ft2.s 36.0 lb/ft2.s
Mixture Velocity, Vm 6.23 ft/s
Liquid Hold up, CL 0.345
Froude Number, Fr 7.25
Mixture Viscosity, µm 1.25E-04
Mixture density 18.99 lb/ft3
Flow Pattern Map Check Flow regimes
L1* 229.1043 Segregated FALSE
L2* 0.0128 Intermittent TRUE
L3* 0.4691 Distributed FALSE
L4* 652.8663 Transition FALSE
Selected flow regime Intermittent
Hydrostatic pressure difference
Liquid Holdup Volume Fraction Horizontal Flow EL(0)
Segregated 0.4926 A -14.85
Intermittent 0.4619 B 15.85
Distributed 0.5077
Selected 0.4619
Check for if greater than CL 0.4619
Liquid Holdup Correction Factor
Liquid velocity number, Nvl 4.50 Flow direction option menu uphill
Correction factor, β downhill
Uphill Flow
Segregated 1.0669
Intermittent 0.1844
Distributed 0.0000
Downhill Flow
All Flow regimes 0.7380
Selected 0.1844
Check for negative values 0.1844
Inclination angle, θ 1.57 radians
B(θ) 1.055
Liquid Holdup EL(θ) EL(0) β B(θ) EL(θ)
For Transition flow -1.9257006375 Segreg. 0.4926 1.0669 1.319 0.650
Selected for transition flow 0.3448 Intermit. 0.4619 0.1844 1.055 0.487
Selected Liquid holdup 0.4874
Two phase density 23.20 lb/ft3
DP due to hydrostatic head 52.85 psi
Pressure drop due to friction loss
Friction factor ratio
y 1.4517
ln(y) 0.3727
S 0.3680
S final 0.3680
Friction factor ratio, fTP/fNS 1.4448
No Slip Reynolds number 157713
Friction factor estimate using Colebrook White equation
Epsilon / D 3.6E-05
Re 157713
Iteration 1 2 3 4 5 6
f 0.0004 0.0261 0.0159 0.0167 0.0166 0.0166
Iteration 7 8 9 10 11 12
f 0.0166 0.0166 0.0166 0.0166 0.0166 0.0166
Iteration 13 14 15 16 17 18
f 0.0166 0.0166 0.0166 0.0166 0.0166 0.0166
Fanning friction factor 0.0042
Two phase friction factor
ft 0.006
DP due to friction loss 3.77 psi
Total pressure drop 56.62 psi
Correction factor due to acceleration
Ek 0.011
Total pressure drop 57.23 psi
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